Process for obtaining valuable products from waxy hydrocarbon stocks



D. A. HERMANSON ET A1. 2,537,999 PROCESS FOR OBTAINING VALUABLE PRODUCTSan. M, i195@ FROM WAXY HYDROCARBON STOCKS 5 Sheets-Sheet l Filed June 9,1948 INSK m. M, E951 D. A. HERMANSON ET AL 2,537,999

PROCESS FR OBTAINNG VALUABLE PRODUCTS FROM WAXY HYDROCARBON STOCKS 3Sheets-Sheet 2 Filed June 9, 1948 INVENTOR.

Jan., "1l-1L E951 A. HERMANSON ET AL PROCESS FOR OBTAINING VALUABLEPRODUCTS FROM WAXY HYDROCARBON STOCKS 3 Sheets-Sheet 5 Filed June 9,1948 material.

Patented Jan. 16, 1951 PROCESS FOR OBTAINING VALUABLE PRODUCTS FROM WAXYHYDROCAR- EON STOCKS Donald A. Hermanson, Plaineld, and John L.

Biles, Woodbury, N. J., assignors to Socony- Vacuum Oil Company,Incorporated, a corporation of New York Application June 9, 1948, SerialNo. 32,018

16 Claims.

This invention relates to a process for preparing valuable hydrocarbonproducts from a wax bearing high boiling mineral oil stock. It isparticularly concerned with a process for obtaining from waxy stocks asubstantially deoiled wax, gasoline and other products boiling lowerthan the original charge stock.

The present process is broadly applicable to the problem of separatingwax and/or petrolatum and the like from hydrocarbon oils insubstantially oil free form. The present process is particularlydirected to the deoiling of crystallizable wax present in high waxystocks such as in Slack wax.

A process commonly employed heretofore for the deoiling of wax is thewell known sweating process wherein the slack wax is chilled in pans tocause congealing of the wax after which the mass is slowly heated toeffect sweating out of `is mixed with a nonviscous non-solvent while inmolten state after which it is cooled to congeal the wax. 'I'hen thecongealed wax is separated from the oil in non-solvent emulsion by meansof a basket type centrifuge lined with a lter material. Such processesinvolve extensive wax recycle to obtain high yield of low oil contentwax.v

It has also been customary in the prior art to employ lter aids such asdiatomaceous earth in powdered form to act as an air in the dewaxing ofoils by the filtration of the wax from the l liquid oil. In such aprocess the liquid oil from which most of the wax has been crystallizedis withdrawn free of the lter aid and the waxy The process has not beenfound practicable as a method for deoiling waxes to obtain oil free wax.As a matter of fact, the waxy material left behind with the filter aidis generally known as Slack wax and contains substantial i amounts ofoil.

In United States Patent 1,278,023", dated Sepwholly absorbed by a solidporous material such as fullers earth after which the fullers earth ischilled to eiect congealing of the sorbefd wax. The fullers earth isthen treated with a suitable oil solvent whereby the liquid oil isremoved leaving behind the wax within the pores of the adsorbent. Thewax is subsequently separated from the solid adsorbent. This process isunsatisfactory because oi the diiiiculty in obtaining satisfactory waxyields thereby and the difficulty of removing this wax from theadsorbent pores without the use of a second solvent for the wax. All ofthese processes provide as products only a deoiled Wax and a foots oilfraction containing varying amounts of residual waxy material.

A major object of this invention is the provision of a process forseparation of wax from oils which not only overcomes the disadvantagesof the prior art processes described above but also provides a gasolinecontaining product instead of ioots oil.

A specific object of this invention is the provision of a novelcontinuous, cyclic process for the deoiling of waxy stocks and theconversion of the oil removed to gasoline containing products by meansof a porous solid adsorbent material.

These and other objects of this invention Will become apparent in thecourse of the following discussion.

The present invention broadly comprises a process wherein the waxy stocksuch as slack wax is brought into intimate contact with a suitableporous particle form solid adsorbent material which is preferablycatalytic in nature as to hydrocarbon cracking reactions. Thetemperature conditions of the contacting are controlled so that the waxyconstituents of the charge stock become congealed in point of time atleast substantially immediately after the initial contacting with theadsorbent whereby the waxy constituents become and remain coated on theouter surface of the adsorbent particles while the noncongealed liquidoil constituents are sorbed into the pores of the adsorbent. Thereafterthe wax is removed froml the surface of the adsorbent leaving behind theadsorbent bearing in its pores the sorbed oily constituents. Theadsorbent is then heated to a temperature at which the Oily constituentsare cracked into lower boiling products which may be removed in thegaseous phase. The adsorbent may then be subjected to a regenerationwherein carbonaceous contaminants deposited during the cracking step areburned off by an oxygen containing gas. Thereafter rlower-.section ofttower ill.

the adsorbent may be cooled and employed again for deoiling waxy stocks.

In order to obtain the optimum yields of wax it is highly important inthis process that the temperature be controlled such that the waxyconstituents in the waxy stock are ina congealed or crystallized stateeither prior to or preferably substantially immediately after beingbrought into contact with the solid adsorbent particles and remaincongealed at least until the step of removing the wax from the adsorbentcommences. It will be readily understood by those skilled in the artthat such expressions as congealed Wax constituents and non-congealedliquid'oil constituents and the like as used indescribing and claimingthis invention do not necessarily mean pure oil-free wax or purewax-free oil since theamount of wax which will congeal from a wax-oilmixture is to some extent dependent upon the temperature of the mixture.For example, if the mixture 4were vcooled to 9G F. waxy constituentsAmight congeal but in the non-congea-led liquid oil there very probablywill be present in non-congealed state some :material which chemicallyshould be classified as a wax. For the purposes of describing .andclaiming 'this` invention a wax which is free of voil shall be taken asmeaning one in which the oil content iszero as determined by the A. S.T. M. method for determining-oil ccntentsof waxy stocks, A. lS. T. M.test number D721-43T.

The invention may be more readily Aunderstood `by reference tothe,drawingsattached hereto in which VFigure 1 isan elevational fiow'plan,partially in section, of a` preferred form of the invention and. Figures2 and 3 are detailed-elevational views, partially `in section, ofcertainportions of the system shown in ligurev 1.

Turning now-to `Figure 1 and considering the invention from-thestandpoint of its operation, a

suitable waxy charge stock such Yas slack wax entering through pipe 9 ispumped by Vpump Iii Athrough heat exchanger l l wherein it is heated toVa temperature slightly above that at which the waxy constituents beginto Vcongeal. vThe heated slack wax then passes via pipe l into the uppersection. ofthe elongated `vertical vessel M. The operation within vesselI4 may be more readily :understood by' reference'together with lFigure l`to Figure v2 which `showsin more vdetail theconstruction of tower It. Acolumn of the-molten slack wax is maintained rwithin section A of thelcoating tower it. A- column of water or other suitable cooling `liquidis maintained within a This liquid should be of greaterldensity' thanthe slack waxrancl a non- .solvent `as to vboth wax and oil. The watervin that-portion ofthe tower it just below the slack wax column is-maintainedsat a temperature suffi- Ciently high to `avoid congealing ofwax at thevinterface between .the slack wax and water columns. Thisisaccomplished by circulating .water through -pipe il intoand throughh-eat exchanger i8 and `back into the water column via'pipe i9 justbelow the interface. Cold water enters the water `column via pipeZtibelow .the level of warm water .outletnpipe il. Particle form porousadsorbent `material which may preferably be of spherical :formfentersthe tower M from supply hopper I it viaverticalpipe 2 I- at about thesame temperature -as theslack wax or at asomewhat .lower temperature.Inrgeneral, the inlettemperature of the adsorbent shouldfusually bebelowabout 100 F. and

preferably below about .80 F. The rate of introof the height of theoutlet end of pipe 2i from nscribed hereinafter.

' tanks 33 or 38.

,adsorbent to the desirecllevel.

conical spreader 22 and by rotation of spreader 22. The spreader isrotated by means of gears 23l shaft 24 and motor lit). Upright conicalbailles 25 and 2S supported by rods 2l and 2S are properly positionedbelow the spreader 22 in such a manner as to distribute the particles ofadsorbent uniformly over the entire cross-section of the tower lll. Theadsorbent particles drop downwardly through the column of slack wax andbecome coated on their surface with a film of slack wax. The particlesthen drop into the water column and the cool water acts to congeal thewax constituents on the surface of the particles. When the differencebetween the particle density and vcooling liquid is small, it isdesirable to add some substance such as potassium oleate to the water or.other cooling liquid to lower the interfacial tension at thewater-slack-wax interface. This will prevent hold up of adsorbentparticles at this interface. The particles of adsorbent bearing thecongealedrmaterial on the Isurface thereofesettle tothe vbottom of towerid andare picked up by thel continuous bucket elevator 2S which connectsinto the lower section of tower M. The buckets Glare perforatedon theirbottoms so that the water may Idrain from the adsorbent in the bucketsonce the buckets rise above the level ofthe liquid. column in theelevator shaft. The partiallydrainedadsorbent vis discharged fromelevator v29 through duct onto a movingscreen belt drainer -32 driven bymotor 3d. A drainer of this typegis shown in attached Figure at"landwill be de- The separated water is withdrawn from the drainer 32through pipe 36 to accumulator 6 i. rifhe water may -be cooledinaccumulator-:tl byfmeans of Va cooling fiuidpassing throughcoil'. Coldmake up water maybeintroduced into the accumulator 6l .through pipe Thewater passes from accumulator El `via pipe 35, pump and pipe 2o back to`Vthecoating tower ii. The drained adsorbent materialcoated with thewaxy stock is discharged from drainer 32 into conveyorl. Theadsorbent isdischarged from conveyor 3l' into one of `-the sorption These tanks areseveral in number although only `two are shown. 'The tanks are employedinV cycle, each tank being shut ofi from the conveyor after being lledwith `The `adsorbent-is permitted to stand in the sorption tank whilethetemperature is controlled by means of heat-trans- -fer tubes (not shown)ata level at .which thewax constituents of the slack wax will remaincongealed. A suitable cooling fluid may be supplied to the heattransfer'tubes within each of .the tanks A3&3 via piper-ll and withdrawnvia pipe42. The adsorbent is retained within the -tankor .33 untilsubstantially all of the non-,congealed liquid oil constituents of theslack wax are sorbed from the congealed mass on the .surface'of theparticles into the pores of the particles leaving `substantially onlythe waxy constituents coated on the outer surface ofthe adsorbentparticles. The adsorbent is then withdrawn through outlets 3@ and 39 andconveyed by Ascrew conveyors :i3 and-4d intotheuppersection of the waxmelting tower Aliwhich is maintained substantially filled with a columnof hot water. The operation of the wax melting tank Y12,5 may be morereadily understood-by reference to Figure 3 in conjunction with Figurel. In Figure Sthere is shown in greater detail the wax melting tank 45andthe subsequent drainer 'l0 and wax separating tank 49. The adsorbentparticles drop from conveyor I throughthe column of -hot waterin azigzagpath provided by baflles 46 so that the Wax deposited on the surface ofthe particles is melted olf from the particles and is passed from theupper section of tower 45 via pipe 40 to the wax separator 49. Themolten wax is withdrawn from the upper section of separator 49 via pipe5|] and the separated water is returned via pipe |09, pump 5| and pipe52 to the lower section of the wax melting tower 45. The water ismaintained substantially above the melting point of the Wax by means ofthe heating coil 53 within separator 49. The adsorbent particles whichstill retain the liquid oil within the pores of the particles arecarried from the bottom of tower 45 in a water stream via conduit 54 anddischarged onto the moving screen drainer F56. The screen 65 is acontinuous screen which passes over rollers II2 and H3, the roller |I3being driven by motor II4 through belt I I5. The screen ES is of suchmesh size as to permit passage of water therethrough while retaining theadsorbent particles. A pan 61 is provided to catch the water passingthrough the screen. This water passes via pipe B8 into accumulator 49from which it is returned via pipe. |09, pump 5i and pipe 52 to themelting tank 45. Additional warm make up water is added to theaccumulator through pipe 'I9'. The drained adsorbent material passesfrom the end of moving screen 55 into duct 'II by which it is deliveredinto a purging apparatus It@ which may be a moving screen similar tothat shown in chamber 10, which screen is driven by motor IZI'. Asuitable purge gas such as steam or heated flue gas may be introducedvia pipe V22 and caused to jet down on the adsorbent on the movingscreen so as to purge additional water from the catalyst. The purge gasmay be withdrawn from the purging apparatus via pipe |23 while the waterremoved from the adsorbent passes via pipe I 24, pump |25 and pipe |26to pipe 58 leading to accumulator 4Q. The purged catalyst drops throughduct |21 into conveyor |28 by which it is transferred to a crackingreactor supply hopper |29. The adsorbent bearing the oily constitulentsthen passes downwardly through gravity feed leg |30, seal Zone IBI andpipe |32 into the reactor |33 wherein it is mixed with hot regeneratedadsorbent of similar type in such proportions as to provide a mixturetemperature suitable for converting the sorbent oily constituents tolower boiling gasoline products. The hot regenerated adsorbent isobtained from hopper |32I from which it flows via gravity feed leg |33into seal zone |40 and then via pipe |39 into reactor |33. An inertgaseous blanket, for example of ue gas or steam, is maintained in sealzones 53| and |40 to prevent escape of hydrocarbon gases through feedlegs |39 and |38. The converted hydrocarbon products are withdrawn ingaseous phase from the lower section of the compact adsorbent column inreactor 53 via pipe |41, and may be fractionated in conventionalequipment. The spent adsorbent now substantially free of oilyconstituents but bearing a carbonaceous contaminant deposit, is purgedfree of hydrocarbon gases by means of an inert purge gas, for examplesteam or iiue gas, entering at |42 and is then passed from the reactorvia pipe M3 to conveyor |44. The adsorbent is transferred by conveyor|44 to regenerator i415 in which it is contacted with air introduced atMt to burn off the contaminant deposit. The combustion products arewithdrawn from regenerator I 45 via pipe I4?. The temperature of theadsorbent may be controlled below a heat damaging level during`regeneration by means of a cooling uid passed.`

through heat transfer tubes (not shown) within the regenerator. The heattransfer medium may be supplied to the tubes via conduit I 48 andwithdrawn therefrom via conduit |49. In general clay type adsorbentsshould be controlled below about 1200o F. and synthetic gel typeadsorbents below about l400 F. during regeneration to prevent permanentloss in activity. The regenerated absorbent is passed from the lower endof the regenerator |45 via pipe I 5I). A portion of the hot regeneratedadsorbent passes to conveyor I5I by which it is transferred to thereactor supply hopper I3?. The remaining portion of the regeneratedadsorbent passes via pipe |53 to conveyor |58 by which it is transferredto the cooler-hopper H0. In hopper IIE the adsorbent is cooled to atemperature suitable for its reuse in the coating tower I4. In general,the adsorbent should be cooled to a level below about 100 F. andpreferably below about F. The cooling may be accomplished by introducinga cold gas into the bed of adsorbent in the cooler via pipe |55 andpassing the gas through the bed. The gas may be withdrawn from thecooler through pipe |56. The cooled adsorbent then passes via pipe 2| tothe coating tower I4.

The conversion system shown is of the continuous type wherein theadsorbent, preferably a cracking catalyst, moves through the reactor andregenerator chambers as a compact column of particles. The operatingconditions Within the reactor I 33 will vary depending upon the activityof the catalyst employed (if it is a catalyst) the particularcharacteristics of the oily constituents sorbed on the cool adsorbentcharge, the reaction involved and the products desired. In general, ithas been found desirable to maintain the pressures within a rangevarying from below atmospheric to about 200 pounds per square inch.Pressures of the order of 5 to 50 pounds per square inch gauge arepreferred. The temperature for the conversion for cracking operationsmay vary from about 800 F. to 1100 F., temperatures of the order of 850F. to 100()0 F. being preferred where gasoline is the desired product.Where non-condensible gases are the principal desired product somewhathigher temperatures may be employed. Theratio of contact material tohydrocarbon throughput for the reactor may vary from about 1.0 to 40parts by weight of adsorbent per part of hydrocarbon charge. The ratioof fresh hot regenerated adsorbent introduced via pipe |39 to cooleradsorbent, bearing sorbed oily constituents, introduced via pipe |32should be so controlled that the resulting temperature of the mixture issuitable for accomplishing the desired hydrocarbon conversion. The exactratio used may be varied somewhat by control of the temperature of thehot regenerated adsorbent and by preheating the oil bearing adsorbentbefore its introduction into the reactor I 33. It has been foundpreferable to employ about 2 to l0 parts by weight of fresh hotregenerated adsorbent per part of the cooler adsorbent bearing the oilyconstituents.

In some operations it may be desirable to add additional liquid orvaporiaed hydrocarbon charge into the reactor |33 via conduit |60 to becracked concurrently with the oily constituents on the adsorbent fromhopper |29. The: mixed conversion products are withdrawn together` viaconduit |4I.

While the above described arrangement for converting the oilyconstituents to lower boiling acerbes products represents a preferredform of this invention, the invention not considered to be limitedthereto. The conversion reaction may be strongly catalytic or mostlypyrolytic depending on the nature of the par'icular adsorbent emnployed. Moreover, the adsorbent may be heated to the conversiontemperature by means other than that described above. For example, itmay be heated by mixing with a hot inert heat carrying mate 1ia-l whichmay be later separated from the regenerated adsorbent. Also theadsorbent may be heated by means of a suitable heat exchange fluidpassed either in direct or indirect heat transfer relationship with theadsorbent particles. The adsorbent may be heated by partial oxidationand burning of the oily constituents thereon. The adsorbent may passthrough the reaction zone as a compact stream, a stream of suspendedparticles or as a fluidized bed. On the other hand the adsorbent may becharged to a suitable vessel wherein it remains in place during theheating, hydrocarbon conversion and adsorbent regeneration steps. Insome operations wherein the reaction is more pyrolytic than catalyticand wherein the amount of carbonaceous contar ant deposited on theadsorbent is small, the adsorbent may be cooled and reused in thecoating tower without regeneration after each reaction step. When aftera number of cycles a substantial contaminant deposit has accumulated, itmay then be removed by burning. .all of these and other modificationswhich will be apparent to those skilled in the art are considered to bewithin the broad scope of this invention.

The invention is also not to be considered as limited to the particularmethod or coating the adsorbent with waxy stock and for recovering thedeoiled wax described hereinabove. In an alternative method instead ofeirecting the congealing of the wax after Contact with the ad sorbent,the waxy constituents oi the charge stock may be caused to congeal atleast partially so as to provide a soft pasty mass into which particlesof adsorbent are pressed. rIhen ater the mass has been maintained incongealed state for sufiicient time for sorption oi the oilyconstituents into the pores of the particles, the wax may be melted toseparate from adsorbent particles. This and other methods for coatingthe waxy stock on the adsorbent are shown and broadly claimed incopending application Serial Number 31,948, filed in the United StatesPatent Onice June 9, 1943, in which one ci the present applicants isapplicant. Any ci the methods described in that application may beemployed in the process of this invention.

It will be readily understood that apparatus and methods other than thatshown in Figure 1 may be employed to accomplish the transfer cimaterials between vessels, the adsorption step and the draining and waxmelting and oil recovery steps. Moreover, the removal of wax from thesurface of the adsorbent particles may be accomplished by methods otherthan by the melting of the wax. For example, the wax may be removed fromthe particles while in solid form by mechanical attrition. This lattermethod is particularly applicable when the wax is of brittle texture andwhere the adsorbent particles are spherical in form. One method foraccomplishing the mechanical separation is to rotate the adsorbentparticles in a closed drum for a period of time to crack oli the brittlewax. The particles of wax may then be separated from the adsorbent-particles by elutriation, i. e. suspension in a stream of gas the iiowrate of which is controlledto carry one the wax particles withoutentraining the adsorbent.

A wide variety of adsorbent materials may be employed in the process cithis invention. For example, bauxites, fullers earth, synthetic silica,alumina or silica and alumina gel catalysts and other materials ofsimilar porosity. Certain porous sorptive silica glasses such as aredescribed in United States Patent 2,106,744, issued February 1, 1938, toHood et al. may be employed. In general, the pore size oi the adsorbentmate` rial should be adapted to eiiect rapid sorption thereinto of theoily constituents of the waxy charge stock. The adsorbent particlesshould be of substantial size as distinguished from powdered adsorbents.When powdered adsorbents of size less than about mesh Tyler are employedthe waxy constituents tend to be sorbed into the pores along with theoily material before complete congealing of the waxy constituents can beaccomplished thereby preventing the desired separation. In general, ithas been found that the adsorbent particles should be broadly at leastabout 0.01 inch and preferably at least about 0.022 inch and less thanabout 0.5 inch average diameter. A preferred adsorbent is a syntheticsilica-alumina gel catalyst in spherical form prepared in i mannerdescribed in U. Patent 2,384,946, issued September 18, 1945, to MiltonM. Marisic.

In conducting the methods described in con` nection with Figures 1, 2and 3, the temperature of the waxy stock brought into initial contactwith the adsorbent should be only several degrees above that at whichthe waxy constituents will commence to congeal. The temperature of thecooling iiuid employed to cause the congealing of wax constituents andto maintain them congealed during the sorption period will. of course,vary somewhat depending on the melting point of the waxy constituentsinvolved. For many operations a cooling water temperature of about 70 F.has been found satisfactory. The operation should be conducted so as toeiiect congealing of the waxy constituents as soon as possible after theinitial contacting with the adsorbent. The waxy constituents should becongealed at least within about l0 minutes of the initial contaoting andpreferably within less than one minute thereof.

The ratio of adsorbent to waxy charge stock employed will depend to someextent upon the oil sorption capacity of 'the adsorbent, the percentageof oil present in the waxy stock and other operating variables. Ingeneral, for synthetic gel catalysts the ratio should be o1 the order of0.5 to l0 pounds of adsorbent per pound of waxy stock. In any case,suiiicient adsorbent should be employed to sorb substantially all oi theoily constituents in the waxy charge.

The length of time to be devoted to the sorption period during whichnon-congealed liquid constituents are sorbed into the pores of theadsorbent will vary depending upon the thiclr ness of the waxy stockcoating on the adsorbent particles and upon the particular adsorbentinvolved and the viscosity and molecular size of the oily constituentsunder the sorption temperature conditions required to maintain the waxyconstituents in a congealed state. In general, it has been found thatwith adsorbent particles of about 0.09 to 0.19 inch average diameter andhaving a porosity similar to a synthetic silica-alumina gel catalyst thelength of the sorption period should 9 be at least about 0.1 hour andpreferably from 1 to 24 hours.

In general the average thickness of the waxy stock coating around eachadsorbent particle should be less than about 0.1 inch and preferablyless than about 0.05 inch.

As an example of the process of this invention the production of adeoiled waxy product and of a gasoline containing product from a waxymineral oil stock by the general method shown in Figure 1 may beconsidered. The waxy charge stock was a paraiiinic petroleum stockhaving a melting point of 116.9 F. as determined by the test procedurerecommended by The American Society for Testing Materials, test numberA. S. T. M. D-87-42 and an oil content of 19.2 as determined by A. S. T.M. tentative test number D-721-43T. The adsorbent employed was a synthetic silica-alumina gel bead catalyst prepared by the method describedin United States Patent 2,384,946, dated September 18, 19115. The catalyst had a bulk density of about .'74 as determined by pouring thecatalyst into a measured container and weighing. The individual particledensity was about 1.15. The catalyst particle size was about 0.09 to0.19 inch average diameter. The catalyst beads were dropped through acolumn of molten waxy stock one inch in depth and maintained at about126 to 183 The weight ratio of catalyst to waxy stock charge was about3.5 to 1. The catalyst beads bearing a coating of waxy stock thendropped through a column of cooling water maintained at about 70 F.About 0.3 to 0.5% potassium oleate was added to the Water to reduce theinterfacial tension at n the water wax interface. The catalyst bearingthe congealed coating of waxy stock was permitted to stand for aboutfour hours at about 80 F. after which the wax remaining on the surfaceof the particles was removed by mechanical attrition. The recovered waxhad a melting point of .l2-5.3 F. and an oil content of 3.2% by weightand the yield of recovered wax amounted to 58% by weight based on thewaxy stock charge or d 72% by weight of the wax present in the charge asdetermined by A. S. T. M. test method D-721-43T. By way of a comparisonthe yield of wax obtained by the method described above using a minimumcooling water temperature of 70 F. amounted to 83% by weight of theyield of wax obtained by solvent deoiling the same waxy stock employingbenzol-methyl ethyl ketone as the solvent at a temperature of 0 F. Thewax obtained by the solvent deoiling process contained 2.4% by weightoil. The adsorbent subu stantially freed of waxy constituents containsabout 12% by weight of an oily paraflinic stock somewhat similar tofoots oil although containing less waxy material and may be purgedsubstantially free of water and mixed at about 100 F. with about 2.5 to3.0 times its weight of hot regenerated catalyst entering the reactionzone at about 1100" F. whereby it is heated to a suitable hydrocarbonconversion temperature. A heated gas oil charge entering at about 850 F.may be passed through the catalyst charge in amount controlled toprovide an overall catalyst to hydrocarbon oil charge ratio of about 2parts catalyst to one part total oil charge to the reactor. The reactionpressure is about 5 pounds per square inch gauge. Gasoline containinghydrocarbon products may be withdrawn in gaseous phase from the reactorand the spent catalyst may be separately withdrawn at about 800 F. Thespent catalyst is regenerated by burning the 10 contaminant and aportion of the regenerated catalyst is cooled to about F. and recycledto the coating tower.

In another experiment conducted similarly to the one just described thesorption period was increased from 4 to 20 hours and the catalyst towaxy oil charge ratio to the coating tower was decreased from 3.5 toabout 1.4. The wax yield was increased to 61% by weight of the originalwaxy charge stock but the oil content in the recovered wax increased toabout 6.7% of the wax. The catalyst after removal of wax from itssurface contained about 28% by weight of oily parafnic material. Thisamounted to a catalyst to oil ratio of about 3.5 to one by weight whichis a satisfactory ratio without addition of extraneous oil charge orcatalyst in the cracking step. Thus, the catalyst may be heated alone toabout 850 F. by means of a heat exchange fluid to crack off the sorbedoily constituents.

It should be understood that the specic details of operation and ofapparatus arrangement and the speciiic modifications of this inventiongiven hereinabove are intended as exemplary and the invention is not tobe construed as being limited thereto or otherwise limited except aslimited by the following claims.

We claim:

l. The method of obtaining a deoiled waxy product and a gasolinecontaining product from a wax bearing high boiling mineral oil whichcomprises: subjecting the wax bearing oil to an intimate contacting witha suitable particle form solid adsorbent material of at least 0.01 inchaverage diameter, maintaining the temperature' during at least most ofsaid contacting at a level at which wax constituents of said wax bearingoil are congealed beginning at a time falling within the period of priorto the initial contacting to substantially immediately after the initialcontacting of the liquid with the adsorbent, whereby the congealed waxconstituents remain deposited on the surface of said adsorbent and thenoncongealed liquid constituents are sorbed into the pores of saidadsorbent, thereafter removing the wax constituents from the surface ofsaid adsorbent while leaving the non-congealed liquid constituentswithin the pores of said adsorbent, heating the adsorbent containingsaid liquid constituents in the absence of said removed wax constituentsto a temperature at which said liquid constituents are converted to alower boiling gasoline containing product and separating said productfrom the adsorbent.

2. A cyclic process for removing oily constitu ents from a waxyhydrocarbon stock which comprises: subjecting said waxy stock to anintimate contacting with a particle form solid adsorbent material madeup of particles having an average diameter Within the range about 0.022to 0.5 inch, maintaining the temperature of the waxy stock during atleast most of said contacting at a level` at which waxy constituents ofsaid stock are precipitated beginning at a time falling within theperiod of any time prior to the initial contacting to not more than 10minutes after the initial contacting of the liquid with the adsorbent,whereby the non-precipitated liquid constituents are sorbed into thepores of said adsorbent while the precipitated waxy constituents remaindeposited on the outer surface of the adsorbent particles, thereaftereffecting removal of said precipitated waxy constituents from saidadsorbent leaving the oily constituents sorbed in the pores of theadsorbent particles, heating the adsorbent in the absence ofc,v saidremoved waxy constituents to a temperature at which said oilyconstituentsl are converted to lower boiling hydrocarbon products,withdrawing said lower boiling products in the gaseous phase from thesolid adsorbent, cooling the adsorbent particles and againcontactingthem with waxy stock as aforesaid.

3; The method of preparing a gasoline containing yproduct and deoiledwax from a waxy mineral oil stock which comprises: subjecting said waxystock to an intimate contacting with particle form solid adsorbentmaterial having an average particle diameter of at least 0.01 inch,maintaining said waxy stock in contact with said adsorbent for a periodof at least 0.1 hour, under conditions at which at least most of thewaxy constituents in said waxy stock are congealed whereby thenon-congealed liquid constituents of said waxy stock are sorbed into thepores of said adsorbent particles while the congealed waxy constituentsare left deposited upon the surface o said adsorbent particles,effecting removal of the congealed waxy constituents from said adsorbentparticles in a separate zone while leaving substantially all of saidliquid constituents still sorbed in the particle pores, heating theadsorbent particles in the absence ofthe separated waxy constituents toa temperature suitable for conversion of said sorbed liquid constituentsto a lower boiling gasoline containing product, separating the gasolinecontaining product in gaseous phase from the solid' adsorbent, coolingthe adsorbent to a temperature suitable for contacting the waxy chargestock as aforesaid and again contacting it with a waxy charge stock.

4. A cyclic process for converting a high boilingl waxy mineral oilstock to deoiled wax and gasoline containing products which comprises:intimately contacting the waxy oil stock with a particle form solidadsorbent material suitable for use as a hydrocarbon cracking catalyst,said material'consisting principally or particles of at least 0.01 inchaverage diameter, substantially excluding the sorption of the waxyconstituents in said mineral oil stock into the pores of said adsorbentparticles by maintaining said waxy constituents in congealed form whilepermitting the non-congealed liquid constituents to be sorbed intothepores of said adsorbent, and after substantially all of said liquidconstituents are sorbed in the pores of said adsorbent eiiecting aseparation of the adsorbent bearing said liquid constituents from saidwaxy constituents in a separate Zone, heating the catalyst in theabsence of the separated waxy constituents to a temperature suitable foreffecting conversion of said sorbed liquid constituents to lower boilinggasoline containing products, maintaining said catalyst at the suitableconversion temperature to effect said conversion with a resultantdeposition of carbonaceous contaminant on said catalyst, separatingthe-gasoline containing products in the gaseous phase from said solidcatalyst, subjecting the used catalyst to contact with air to effectremoval of said'contaminant by burning at a controlled elevatedtemperature, cooling the catalyst and again employing it for contactingwaxy mineral oil stock as aforesaid.

5. The method of separating oily constituents from waxy constituentspresent in a waxy hydrocarbon stock which comprises: coating said waxystock onto the surface of particles of solid adsorbent material ofgreater than about 0.01 inch average diameter, permitting the adsorbentparticles to remain coated with said waxy stock for a period within-thevrange 0:1`V to 2li hoursand* maintainingk the temperature of thewaxy-'stock' during substantia'llysaid` entire period-beginning at leastsubstantially? immediately after" initialv contact with said adsorbentAata level at which waxy constituents in said stockv ares congealed'Vwhereby the non-congealedr liquidV constituents are sorbedA into theVpores of saidadsorbent'particles while the` congealed waxy constituentsremain on the surface of'said particles, thereafteru effecting removalof said waxy constituents'from the surface of said adsorbent particleswhile leav'- ing sorbed said non-congealedliquid constituents;` mixingthe adsorbent bearingsorbed liquid oily;y constituents with asuicientamount of notadsorbent ofsimilar'type to heat it to" atemperature suitable for the conversion' of saidsorbedV liquid oilyconstituents to lower'boiling products',r eecting substantialseparationof'said lower boiling products fromV the used adsorbent'uponwhich a carbonaceous contaminant has beendeposited', effectingV removalof said'` contaminant from theA used adsorbent andreusing atleast aportion of'v the adsorbent after said contaminant removal as theadsorbent on which said waxy stockzis coated as aforesaid.

6; The method for converting a waxymineral cil stock into gasoline andwax products which comprises: coating the waxy mineral oil stock ontothe surface of particlcsof solid adsorbent material of greaterthaniabout G;01 inch average particle diameter and suitable as ahydrocarbon cracking catalyst,` substantially'immediately chilling thecoated adsorbent to eiectcongealingof wax constituents in said waxystock' coated'on said adsorbent particles, permitting theadsorbentparticles to remain coated4 with said'waxy stock whilemaintainingY saidVv waxy'constituents in congealed form untilsubstantially allof the non;- congealed liquidconstituents ofsaidwaxystock arel sorbed into the pores of saidiparticles leavingithecongealed waxy constituents onV the surfacezof' said particles,thereaftereiectin'g removal ofsa'idA wax constituents from the surfaceoi said adlsorbent particles while leaving the non-congealed` liquidoily constituents still sorbed intheporesi of said adsorbent particles,`heating saidadsorbent bearing` sorbed liquid'oily constituents toatemperature at which said liquid oilyv constituentsare catalyticallyconverted to vlower boiling gasoline containing products,l effectingsubstantial separation of said lower boilingvproducts from' the usedadsorbent upon which a, carbonaceous" contaminant has been .deposited asa result of` the conversion ofr said liquid oily constituents, effectingremoval ofv said `contaminant from. the used adsorbent, cooling theadsorbent and reusing,v it as the adsorbent upon which said waxyAmineral oil stock is coated as aforesaid.

7. The method of deoiling slack' wax stockswhich comprises I, coatingsaidslack wax stock in liquid form onto the surfaceof particlesof'adsorbent material in an adsorbentccating zone, said adsorbentparticles being of 'at least 0.01' inch average diameter, chilling., thecoated adsorbent particles to eiTect precipitationcf.wax'constituL entsinr said slack `wax stock'coatedthereonV at least within about 10minutesof the beginning` of the adsorbent coating,` maintainingv the waxconstituents inprecipitated-form on-said adsorbent particles for aperiod-of at least'fkl hour. until substantially all of thenon-precipitated 1iq uidA constituents of said slack wax aie sorbed intothe pores of said adsorbent par-ticlesv leaving thel precipitated waxenthe surfaceJ or-said particles.

`effecting removal of the precipitated wax from the surface of saidadsorbent particles while leaving the liquid constituents still sorbedin the pores of said adsorbent particles, separately passing theadsorbent bearing the sorbed liquid constituents through a confinedconversion Zone in admixture with a sufficient quantity of hotregenerated particle form adsorbent of similar type to heat it to atemperature suitable for conversion of said sorbed liquid constituentsto lower boiling hydrocarbon products, separating the lower boilingproducts in the gaseous phase from the used adsorbent, passing the usedadsorbent through a confined regeneration none while contacting ittherein with a combustion supporting gas at a controlled elevatedtemperature to remove contaminant deposits from the adsorbent, cooling aportion of the hot regenerated adsorbent and recycling it to saidcoating zone and utilizing the remainder of the hot regeneratedadsorbent as the hot regenerated adsorbent which is mixed with theadsorbent bearing sorbed liquid constituents as aforesaid.

8. The cyclic process for providing deoiled wax `and gasoline containingproducts from a wax-oil charge stock by means of a particle formcatalytic adsorbent material which comprises: subjecting said wax-oilstoel; to an intimate contacting with the particle form adsorbentcatalyst made up of particles of average diameter within the range about0.022 inch to 0.5 inch and having a substantial catalytic activity forhydrocarbon cracking reactions under conditions of temperature whereinthe waxy constituents of said stock become congealed at the latestwithin about minutes of the beginning of said contacting, continuingsaid contacting until substantially all of the non-congealed liquidconstituents of said stock are sorbed into the pores of said adsorbentparticles while leaving the congealed wax on the surface of saidparticles, effecting the removal of the wax from the surface of saidparticles, and collecting the same as deoiled wax product, mixing thecatalyst bearing sorbed oily constituents `with hot catalyst of similartype to heat it to a suitable temperature for the conversion of saidoily constituents to a lower boiling gasoline containing hydrocarbonproduct, passing the mixture through a confined conversion zone toeffect the conversion of said oily constituents, effecting a separationof the lower boiling hydrocarbon products from the used catalyst bearinga contaminant deposit, passing the separated used catalyst through aconi-ined regeneration zone while contacting it therein with acombustion supporting gas at a controlled elevated temperature to removecontaminant deposits from said catalyst, utilizing a portion of theregenerated catalyst for contacting cool catalyst bearing sorbed liquidconstituents from said wax-oil stock as aforesaid and cooling theremainder of said regenerated catalyst and utilizing it for contactingsaid wax-oil stock as aforesaid. I

9. The method for producing deoiled wax and a gasoline containinghydrocarbon product from a wax-oil petroleum charge stock whichcomprises: encasing particles of adsorbent catalyst having an activityfor hydrocarbon cracking and having an average diameter of at least 0.01inch in said wax-oil petroleum stock under conditions of temperaturesuch that at least most of the wax constituents of said stock are incongealed state substantially from the beginning of the contact of thestock with the catalyst particles, maintaining said catalyst particlesencased in saidw wax-oil "stock until substantially all thenon-congealed `oily constituents of said stock are sorbed into the poresof the catalyst particles leaving the wax constituents of said stock incongealed state on the surface of the catalyst particles, eiecting aseparation of the wax constituents of said stock from the surface ofsaid particles and cooling the same as deoiled wax products, passing theparticle form catalyst after separation from the wax constituents butstill bearing the sorbed oily constituents downwardly through a confinedconversion zone maintained under a temperature suit- -able for thecracking conversion of said oily constituents to lower boiling gasolinecontaining hydrocarbon products, moving said catalyst through said zoneas a downwardly gravitating substantially compact column withdrawinggaseous conversion products from said conversion zone, separatelywithdrawing the particle form catalyst bearing a contaminant depositedduring the hydrocarbon conversion from the lower section of saidconversion zone, passing the used. catalyst through a connedregeneration Zone in contact with a combustion supporting gas to effectremoval of said contaminant by burning while controlling the temperatureof said catalyst above that minimum required for practical contaminantburning rates and below a temperature at which said catalyst wouldsuffer permanent loss in catalytic activity, withdrawing the hotregenerated catalyst from the regeneration zone cooling at least aportion of said regenerated catalyst to a temperature below about F. andagain encasing said catalyst in said wax-oil stock as aforesaid.

10. The method for removing oily constituents from a waxy hydrocarbonstock which comprises: subjecting said waxy stock to an intimatecontacting with a particle form solid adsorbent material comprisingparticles of at least 0.01 inch average diameter, effecting sorption ofthe liquid oily constituents of said waxy stock into the pores of saidadsorbent particles while substantially preventing sorption of the waxconstituents by maintaining the temperature during said contacting at alevel at which the wax constituents become congealed, effecting theseparation of the wax constituents from the surface of said adsorbentparticles, passing said adsorbent particles bearing the liquid oilyconstituents of said waxy stock in the pores thereof during a confinedconversion zone in admixture with a substantial quantity of hot particleform heat carrying mate- `rial to heat it to a temperature suitable forthe conversion of said sorbed cily constituents to lower boilingproducts, eiiecting the separation of said lower boiling products fromthe used adsorbent material, reconditioning at least a portion of saidadsorbent material to put it in condition for reuse in contacting saidwaxy stock and then 'again `using the reconditioned adsorbent materialfor contacting said waxy stock as aforesaid..

11. The method of deoiling waxy hydrocarbon stocks which comprises:coating the surface of porous solid adsorbent particles of at least 0.01inch average diameter with said waxy stock at a temperature justslightly above that at which the waxy constituents begin to crystallizesubstanfonthesurface of the particles, thereafterimelting 'the 'waxfromthe surface of the sorbentparticles Aand collecting themelted waxseparately of the radsorbent particles and sorbed oily constituents,:passing the adsorbent particles bearing the sorbed .oily constituentsthrough a conned conversion zone under temperature conditions suitablefor eiecting the conversion of said oily constituents to lower boilinggasoline containing hydrocarbon products, separating the gasolinecontaining hydrocarbon products from the used sorbentparticles,"reconditioning at least a portion of the used adsorbentparticles and returning the reconditioned particles as the adsorbentcharge to said coating zone.

v12. A method for preparing deoiled wax and gasoline hydrocarbonproducts from wax-oil vlpetroerufn stocks which comprises: maintaining-`-a liquid column of said wax-oil stock at a temperature slightly abovethat at which the waxy constituents begin to congeal, maintaining below.and contiguous with the bottom of said column or" wax-oil stock acolumn of water, maintaining a short length of the column of waterimmediately below the column of wax-oil stock at a temperature near thatof the wax-oil stock and maintainving 4the remainder of said column ofwater at a temperature at which the waxy constituents of said stock willcongeal, dropping particles of solid adsorbent having an averagediameter of @at -least 0.01 inch and having a substantial catalyst`activity for the cracking conversion of hydrocarbons downwardly throughsaid column of wax-oil stock to cause said particles to become coatedwith wax-oil stock, causing the coated particles to drop downwardly.into and through said 'column of water to `cause the waxyconstituentsin the stock coating said particles to Vbecome congealed,removing the particles bearing thecoating of wax-oil stock fr m saidwater Acolumn and permitting the particles to stand r at a temperaturebelow the congealing temperature of said waxy constituents untilsubstantialyly all the non-'congealed constituents oi the wax- -oilstock coating said particles are sorbed into the pores of said adsorbentparticles while leav- .fin'g the Iwaxy constituents on the surface ofsaid particles, then Vcontacting the adsorbent particles with heatedwater to melt and to remove the :waxy Aconstituents from the surface ofsaid particles while leaving the non-congealed constituents of thewax-oil stock sorbed in the pores of said particles, purging saidadsorbent particles substantially free of water by means of a suitablepurge gas, mixing said purged particles of adsorbentbearingnon-congealed constituents of said wax-oil stock with asubstantial quantity of hot regenerated adsorbent particles of similartype to provide a heated mixture of adsorbent Lat .a temperaturesuitable for eiiecting the conversion of said sorbed oily constituentsto lower boiling gasoline containing products, passing the mixedadsorbent with a substantial quantity of contact particles downwardlythrough a coniined conversion zone wherein the oily constituents areconverted, withdrawing the gasoline containing oily constituents in thegaseous phase from said conversion zone, separately withdrawing sorbentV'material bearing a oarbonaceous contaminant .deposited during thehydrocarbon conversion fromthe lower section of said conversion zone,4passing the used adsorbent through a conned -regeneration zone incontact with a combustion supporting gas to effect burning of thecontaminant deposit,f controlling the temperature of said adsorbentduring the regeneration belowxa tempera-ture at which it would 'sufferpermanent heat damage to its porosity and catalytic activity, returninga portion of the hot adsorbent to said conversion zone, cooling anotherportion of said hot regenerated adsorbent to a temperature below aboutreturning the cooled adsorbent to said liquid column of wax-oil stock.

i3. A method for deoiling wax-oil petroleum stocks which comprises:maintaining a rliquid column of said wax-oil stock at a temperatureslightly above that at which the waxy constituents begin to congeal,dropping particles vof solid adsorbent catalyst material oi at least0..'01 inch average diameter which are suitable foreffecting hydrocarboncracking conversions and suitable for sorbing liquid oil in its poresthrough column to deposit a ilm of said waxy stock on the surface ofsaid catalyst particles, `immediately dropping said catalyst particlesinto a bath of a suitable cooling liquid maintained at a temperaturesuitable for congealing the waxy constituents of said wax-oil stock,permitting the adsorbent particles to remain coated with said wax-oilstock While maintaining the waxy constituents in a congealed state`until substantially all the non-congealed constituents are sorbedintothe pores of said particles, thereafter eiecting removal of the waxyconstituents from the surface of said catalyst particles while leavingsaid non-congea'ed liquid constituents sorbed in-the pores of saidparticles, passing said catalystl particles bearing sorbed liquidconstituents of said wax-oil stock through a confined conversiorrzonewhile heating it to a temperature suitable for effecting conversion ofsaid liquid constituents to lower boiling gasoline containinghydrocarbon products, separating said lower boiling products from theused catalyst, effecting the regeneration of said used catalyst at anelevated temperature by means of a combustion supporting gas, cooling-at least a portion of the regeneration catalyst and returning it tosaid liquid column of wax-oil stock as the catalyst charge thereto.

14. The method for removing oily constituents nm a itx-xy petroleumstock which comprises:

eeting waxy stoel; to an intimate cong with an inorganic oxide gel.adsorbent 'ng of particles of generally spheroidal shape and of anaverage `diameter of at least about 0.01 inch, wher .3y the waxy stockis coated onto the surface of said adsorbent particles, controlling thetemperature of said waxy stock so that the wax constituents becomecongealed -at the latest substantially immediately after the waxy stockis coated upon said particles, causing the adsorbent coated with thewaxy stocklto stand at a temperature at which said wax constituentsremain congealed until substantially all the non-congealed liquidconstituents of said stock are sorbed into the pores of said particlesleaving the wax on the surface thereof, then removing the wax from thesurface of said adsorbent particles and collecting the removed waxseparately of the adsorbent particles, mixing the adsorbent particlesybearing sorbed non-congealed liquid constituents of said waxy stock:with a-substantial amount of hot regenerated adsorbent of similar typeto heat it to atemperature suitable for eiecting the conversion of saidliquid constituents to lower boiling gasoline containing hydrocarbonproducts, passing the mixed adsorbent as a substantial compactgravitating column of particles downwardly through a confined conversionzone to effect the conversion of said liquid constituents withdrawingthe lower boiling hydrocarbon products from said conversion zone,separately withdrawing the used adsorbent bearing a carbonaceouscontaminant from the lower section of said conversion zone, passing theused adsorbent through a conned regeneration zone as a substantiallycompact column in contact with a combustion supporting gas to burn 01Tsaid contaminant while controlling the temperature of said adsorbentbelow a heat damaging level, withdrawing the regenerated adsorbent fromthe lower section of the regeneration zone, utilizing a portion of thehot regenerated adsorbent for mixing with the cooler liquid constituentbearing adsorbent as aforesaid, cooling the remainder of said hotregenerated adsorbent and again contacting it with said waxy stock asaforesaid.

15. The method for preparing gasoline containing hydrocarbon productsand a deoiled wax product from a wax-oil petroleum stock whichcomprises: intimately contacting the wax-oil stock with a particle formsolid adsorbent in which the average particle diameter is at least 0.01inch and which has a substantial catalyst activity for hydrocarboncracking reaction, substantially excluding the adsorption of the waxyconstituents of said wax-oil stock into the pores of said adsorbentparticles by maintaining said waxy constituents in congealed form whilepermitting the non-congealed liquid oily constituents to be adsorbedinto the pores of said adsorbent, after substantially all of said liquidconstituents are sorbed in the pores of said adsorbent effecting aseparation of the adsorbent bearing said liquid oily constituents fromsaid waxy constituents in a separate Zone, mixing the adsorbent bearingthe liquid oily constituents with a suicient amount of hot regeneratedadsorbent of similar type to heat it to a temperature suitable foreffecting the catalytic cracking of said liquid oily constituents tolower boiling gasoline containing hydrocarbon products, passing themixed adsorbent through a confined conversion zone to effect theconversion of said sorbed liquid oily constituents, separatelyintroducing a vaporized hydrocarbon fraction into contact with saidadsorbent within said conversion zone to effect the catalytic crackingconversion of said hydrocarbon fraction to gasoline containing products,effecting the separation of the mixed hydrocarbon products in thegaseous phase from the used solid adsorbent, passing the used adsorbentthrough a confined regeneration zone in contact with a combustionsupporting gas to burn o contaminant deposited thereon during thehydrocarbon conversion, controlling the temperature of the adsorbentduring the regeneration below a heat damaging level, withdrawing theregenerated adsorbent from said hot regenerating zone, utilizing theportion of hot adsorbent with the cooler liquid oily constituent bearingadsorbent as aforesaid, cooling the remainder of said hot regeneratedadsorbent and again utilizing it for contacting said wax-oil stock asaforesaid.

16. The method for separating oily constituents from waxy constituentspresent in a waxy hydrocarbon stock which comprises: coating said waxystock onto the surface of particles of solid adsorbent hydrocarboncracking catalyst of greater than about 0.01 inch average particlediameter, limiting the average thickness or" the wax coating on saidcatalyst particles to less than about 0.1 inch, permitting the catalystparticles to remain coated with said waxy stock within the range 1 to 24hours and maintaining the temperature of the waxy stock during saidperiod beginning at least substantially immediately after initialcontact with said catalyst at a level at which waxy constituents in saidstock are congealed whereby non-congealed liquid constituents are sorbedinto the pores of said catalyst particles while the congealed waxyconstituents remain on the surface of said particles, thereby effectingthe removal of said waxy constituents from thelsurface of said catalystparticles while leaving sorbed non-congealed liquid oily constituentswithin the pores of said particles, passing the separated catalystparticles bearing the sorbed oily constituents as a substantiallycompact column downwardly through a confined conversion zone inadmixture with a suiiicie-nt quantity of hot regenerated catalysts ofsimilar type to heat it to a temperature at which said liquid oilyconstituents are converted to a lower boiling gasoline containinghydrocarbon product, withdrawing the gasoline containing product in thegaseous phase from said conversion zone, separately withdrawing spentcatalyst bearing carbonaceous contaminant deposit from the lower sectionof said conversion zone, passing said spent catalyst through a confinedregeneration, zone in contact with air to burn the carbcnaceouscontaminant while controlling the temperature of said catalyst below aheat damaging level, withdrawing the hot regenerated catalyst from saidregeneration zone, utilizing portion of the hot regenerated catalyst formixing with the coolel` catalyst bearing said liquid oily constituentsas aforesaid, cooling another portion of said hot regenerated catalystto a temperature below about F. and again coating the cooled catalystwith said waxy stock as aforesaid.

DONALD A. HERMANSON. JOHN L. BILES.

REFERENCES CITED The following references are of record in the ille ofthis patent:

UNITED STATES PATENTS Number Name Date 115,622 Lucas et al June 6, 1871226,001 Riebeck Mar. 30, 1820 1,278,023 Rosenbaum Sept. 3 1918 1,447,297i Day Mar. 6, 1923 1,509,326 Weir Sept. 23 1924 1,568,018 Forrest et alDec. 29, 1925 2,351,793 Voorhees June 20, 1944 2,382,755 Tyson Aug. 14,1945 2,437,222 Crowley Mar. 2, 1948 OTHER REFERENCES Allibone, Journalof the Institute of Petroleum, vol. 27, pages 94-108 (1941).

1. THE METHOD OF OBTAINING A DEOILED WAXY PRODUCT AND A GASOLINECONTAINING PRODUCT FROM A WAX BEARING HIGH BOILING MINERAL OIL WHICHCOMPRISES: SUBJECTING THE WAX BEARING OIL TO AN INTIMATE CONTACTING WITHA SUITABLE PARTICLE FORM SOLID ADSORBENT MATERIAL OF AT LEAST 0.01 INCHAVERAGE DIAMETER, MAINTAINING THE TEMPERATURE DURING AT LEAST MOST OFSAID CONTACTING AT A LEVEL AT WHICH WAX CONSTITUENTS OF SAID WAX BEARINGOIL ARE CONGEALED BEGINNING AT A TIME FALLING WITHIN THE PERIOD OF PRIORTO THE INITIAL CONTACTING TO SUBSTANTIALLY IMMEDIATELY AFTER THE INITIALCONTACTING OF THE LIQUID WITH THE ADSORBENT, WHEREBY THE CONGEALED WAXCONSTITUENTS REMAIN DEPOSITED ON THE SURFACE OF SAID ADSORBENT AND THENONCONGEALED LIQUID CONSTITUTENTS ARE SORBED INTO THE PORES OF SAIDADSORBENT, THEREAFTER REMOVING THE WAX CONSTITUENTS FROM THE SURFACE OFSAID ADSORBENT WHILE LEAVING THE NON-CONGEALED LIQUID CONSTITUENTSWITHIN THE PORES OF SAID ADSORBENT, HEATING THE ADSORBENT CONTAININGSAID LIQUID CONSTITUENTS IN THE ABSENCE OF SAID REMOVED WAX CONSTITUENTSTO A TEMPERATURE AT WHICH SAID LIQUID CONSTITUENTS ARE CONVERTED TO ALOWER BOILING GASOLINE CONTAINING PRODUCT AND SEPARATING SAID PRODUCTFROM THE ADSROBENT.